Treatment of compounded oils



Patented June 4, 1946 ICE.

v i Russell P. Dunmire, Chagrin Falls, Ohio, assignor, 'by mesne assignments, to Buckeye Laboratories Corporation, Cleveland, Ohio, a corporation of hio No Drawing. Original application November 26,

1941, Serial No. 420,595. Divided and this application September 16, 1943, Serial No. 502,641

16 Claims. (01. 252-488) Myinvention is directed to the process of treating. purifying or re-refining compounded oils of the class consisting of mineral oils com-' pounded with an oil-soluble additive substance.

' of the class consisting of mineral oil compounded with an oil-soluble additive substance by subjecting the compounded oil to a process utilizing a combined action of adsorption and distillation.

Another object of my invention is directed to the process of re-refining contaminated or used compounded oils of the class consisting of mineral oils compounded with an oil-soluble additive substance to render same in a state of purification.

Another object of my invention is directed to the process of purifying the contaminated or used compounded oil of the class consisting of mineral oils compounded with an oil-soluble additive substance by subjecting same to a re-reflning process utilizing a combined action of adsorption and distillation, wherein the high boiling point or substantially non-volatile impurities or undesirable constituents are removed by adsorption and the low boiling point volatile impurities or undesirable constituents are removed by distillation.

Another object of my invention is directed to theprocess ofpurifying a contaminated or used compounded oil of the class consisting of mineral oil compounded with an oil soluble additive substance by subjecting same to a re-refining process utilizing the combined action of adsorption and distillation, wherein the distillation is carried out at a temperature in the range of the incipient azeotropic distillation point of the constituents comprising the compounded oils.

Another object of my invention is directed to the process of purifying a contaminated or used compounded oil of the class consisting of mineral oil compounded with an oil soluble additive substance by subjecting the same to a re-refining process utilizing the combined action of adsorption and distillation, wherein the distillation is carried out at a temperature determined by the incipient azeotropic distillation point of the constituents comprising the compounded oil.

Another object of my invention is directed to a.

Another object of my invention is the process I of purifying a contaminated or used compounded oil of the class consisting of mineral oil compounded with an oil soluble additive substance under conditions to give a maximum yield and yet obtain a good purified product.

The term "contaminated as used herein and also in the claims means an oil which is unfit or unsatisfactory for a specific purpose.

Other objects and a fuller understanding of my invention may be had by referring to the following description and claims.

In carrying out my process, the contaminated or used oil to be treated is transferred to a suitable reaction vessel or container which is equipped with a mechanical agitator and which is arranged to be evacuated by any suitable means. The'reaction vessel or container is also arranged to be heated for the purpose of carrying out the process. In other words, the reaction vessel or container comprises a retort provided with a mechanical agitator and is connected to a condensate receiver to carry-out fractional or partial distillation involved in the re-refining process.

To the contaminated orused oil-being treated I add a supply of solid adsorbent material in the retort or steel container. The amount of the solidadsorbent material which is added tothe contaminated or used oil being treated. The

solid, adsorbent material may comprise bone char, carbon black, fullers'earth, etc. The combined mixture of the contaminated or used oil being treated and the adsorbent material is vigorously agitated by mechanical means in the retort under a vacuum preferably in the range of 28 inches to 30 inches of mercury as referred to a 30-inch barometer at sea level. In addition to the adsorbent material, an aqueous medium may be added in the form of water or steam as a sweeping agent.

Generally speaking, all oils are mixtures of various hydrocarbons or of fatty acids, glycerides or other esters. As such, they possess the property of ideal solutions obeying Raoult's law and Henry's law and are governed by the laws of distillation which apply toazeotropic mixtures.

In the re-refining process comprising the combination'of adsorption and distillation, I have found th t the most satisfactory combination of property, color and yield is obtained when the 011 being treated is held at a temperature at which azeotropic distillation of the mixture begins as evidenced by a collection of distillates in the distillate receiver; that is to say, at a temperature at which the first initial fraction of the oil begins to distill oil under the conditions of operation. This temperature at which the first initial fraction of the oil begins to distill oil will be referred to herein as the incipient azeotropic distillation point of the constituents of the oil being treated.

At temperatures materially below the incipient azeotropic distillation point a sufficiently high degree of purification is' not obtained. At temperatures greatly beyond the incipient azeotropic distillation point the results are not completely satisfactory either from the standpoint of property and color of the re-fined product or from that of yield, or from both. The temperature range extends up to a value substantially 100 F. beyond the incipient azeotropic distillation point of the constituents of the oil in its finally treated state and includes an elevated temperature in the range of the incipient azeotropic distillation point of the constituents of the oil in its finally treated state and preferably embraces a range approximately 100 F. on either side of the incipient azeotropic distillation point of the constituents of the oil in its finally treated state.

The treatment at temperatures in excess of approximately 100 F. beyond the incipient azeotropic distillation point leads to discoloration of the final product and also reduces theyield because of the losses by distillation of the oils. The treatment at temperatures less than 100 F. below the incipient azeotropic distillation point gives a satisfactory yield but a sufflciently high degree of purification is not obtained because the maximum effect of the adsorbent is not attained in this low range of temperature.

The mechanical agitation or stirringof the combined mixture of the contaminated or used oil being treated and the adsorbent material in the sealed container brings all of the constituents thereof in close intimate physical contact and the adsorbent material thereby adsorbs the high boiling point impurities or contaminants of the oil being treated which are substantially nonvolatile under the conditions of operation. The heating of the'retort drives off substantially all of the low boiling point volatile impurities by dismore depending upon the temperatures employed in the re-refining process, the amount of the adsor-bent material employed, and the degree to which the oil has been contaminated. The process may also be continuous or intermittent.

In considering the degree of purification or the quality of compounded oils of predominating mineral oil composition, the most important characteristics are generally neutralization value, flash and fire points, viscosity and the analytical determination of the quantity 'of the oil soluble additive substance with which the mineral oil is compounded. Another factor usually considered significant is the color of the treated product, both from the aspect of physical appearance which is of commerccial importance and also since the appearance may indicate the presence or absence of appreciable quantities of oxidation or other products foreign to the normal characteristics of the oil which has been treated. Tables are given below showing the properties of several oils subjected to a treatment utilizing a combined process of adsorption and distillation under vacuum and at different temperatures. For purposes of illustration, I have selected mineral oil compounded with lard oil, mineral oil compounded with a sulfur compound and mineral oil compounded with a sulfur and chlorine compound. The selected oils are widely used in industry and commerce.

It has been found through the years that usually an oil consisting of a single component is not completely suitable for many specific purposes, particularly with the development of modern high-speed heavy duty machinery. For many purposes it is necessary to use an oil or lubricant compounded with a mineral hydrocarbon and a substance soluble in that hydrocarbon to materially improve or accentuate some desirable property. For example, it will be noted that modern Diesel engines are usually lubricated with solutions of detergent materials in mineral oil of low carbon content. For metal working, cutting, broaching, and similar operations, it is usually necessary to use mineral oils compounded with fat, sulfur compounds, chlorine compounds, or mixtures of these compounds; and in many aircraft engine lubricants, it is desirable or necessary to'use mineral oils containing in solution small amounts of oil soluble esters, such as the esters of oxidmed petroleum products and certain phosphoric and phosphorous acids. I have found that the process herein described is suitable for the re-refining of such compounded oils, and is a desirable and economical adjunct to the use of. such compounded oils and lubricants, since many are relatively costly, and since their usefulness is limited by the extent to which deterioration may occur in service. I have also found that the conditions of re-refining may be so controlled that the adsorbent will not remove the oil-soluble active compound dissolved in the oil. That these conditions may be adequately defined and recognized, the fOlIOWillg examples are given to show the limitations involved and the means by which I have defined them.

The Tables I, II and III give the results on a series' of refining operations made on a group of three compounded oils; namely, mineral oils compounded with lard oil, mineral oils compounded with oil soluble sulfur compounds, and mineral oils compounded with oil soluble sulfur and chlorine compounds. These oils are commonly used in the working of metal and are usually referred to in the trade as cutting oils. Thus, the mineral oils compounded with lard oils may be referred to as lard cutting oils, mineral oils compounded with an oil soluble sulfur compound may be referred to as sulfur cutting oils, and mineral oils compounded with oil soluble and chlorine compounds may be referred to as sulfur and chlorine cutting oils.

In Table I are given the results on a series of re-refining operations made on lard cutting oil at the temperatures shown in the column headout for a period of minutes with substantially identical proportions of adsorbent and under substantially identical conditions of vacuum which at various temperatures and the time and vacuum set forth in the previous table. The first column ives the characteristics of the contaminated sulwas maintained at substantially 29.75 inches of 5 fur cutting oil before being subjected to the remercury. The differences in temperatures noted refining process.

Lard cutting oil Original sample 200 1 250 F. 000 r 320" r 300 F 400" r.

Neutr. No 6.6.. 5.5 5.3 4.8. 4.5 4.4 4.2.

e10 380 300 zoo ass.

Dark brown.. Dark brown Light brown Light brown.. Light brown. v18.s.U.v.an00r......... 200 209 21s 22o 222 222 22a. Condensate ior azeotroplcdis- 0 0 .8 2.1 4.6 8.8.

tillation, per cent. Yield oiproduct, percent 94 90 87 82 77 71.

may vary to meet any particular application.

The first column gives the characteristics for the contaminated cutting oil before being subjected to the re-refining process.

As evidenced by the retention of the oil soluble compound as indicated by the analytical determination of the sulfur content, the best yields of a product of greatly improved appearance anddesirability were obtained at those temperatures where azeotropic distillation of the pressure utilized was beginning; namely, approximately at 250 F. At temperatures greatly below this value, that is, below the incipient azeotropic distillation Sulfur cutting oil Neutr. No

Flash point, F.

Fire Point, F.

Color Vis. S. U. V. at 100 F l3 Condensate for azeotropic distillation,

per cent.

Yield of product, percent Dark brown.- Dark brown..

As evidenced by the retention of the oil soluble compound as indicated by the saponification number, it will be observed that the maximum of yields of a product of excellent appearance and of desirable physical and chemical characteristics were obtained at those temperatures where azeotropic distillation at the pressure utilized was begirming; namely, approximately at 300 F. At temperatures greatly below this value, that is, below the incipient azeotropic distillation point, a desirable degree of purification was not observed, while at temperatures greatly above this value, the same eflfects were observed insofar as refining was concerned and in addition, the yields of products were greatly diminished.

The Table II gives the results of a similar series of tests conducted on a contaminated sulfur cutting oil. As before, substantially identical proportions of adsorbent were used in the treatment point, a desirable degree of purification was not obtained, while at temperatures greatly above this value, the same effects were observed insofar as re-reflning was concerned, and in addition, the

yields of products were greatly diminished- Table II shows the results obtained when a series of re-refining treatments were carried out at various temperatures on a sample of contaminated sulfur and chlorine cutting oil. The first column gives the characteristics of the contaminated sulfur and chlorine cutting oil. In each of the subsequent columns, the results are given of the treatment of this cutting oil by a process of re-refining consisting of adsorption and dis tillation where the proportion of adsorbent and the time and vacuum are held substantially constant, the same as in the preceding tables, and where the differences in temperature noted were the only variables.

TABLI: III

Sulfur and chlorine cutting oil 1,33%: 200 1. 250 F. 215 F 300 F 350 F 400 F Neutr. No

0r Vis. S. U. V. at F Condensate ior azeotropic distillation, per cent. Yield 0i product per cent As evidenced by the retention of the oil soluble compound as indicated by the analytical determination of the sulfur content and .the chlorine content, it will be noted that the maximum yields of a product of excellent appearance and of desirable physical and chemical characteristics were obtained at those temperatures where azeotropic distillation at the pressure. utilized was beginning; namely, approximately at 250 F. At temperatures greatly below this value, that is, below the incipient azeotropic distillation point, a desirable degree of purification was not obtained, while at temperatures greatly above this value, the same effects were observed insofar as refining was concerned, and in addition, the yields of product were greatly diminished.

In consideration of the results of the three samples given in Tables I, II and III, it has been shown that in every instance there was a well defined temperature range for best results, and this coincided with the temperature at which distillation commenced of the azeotropic mixtures of the hydrocarbon compounds entering into the composition of the mineral oil which constitutes the major constituent of the compounded oils. When low temperatures were employed, that is. temperatures at which no azeotropic distillation could occur under the conditions of operation, I have found that in nearly all cases an insufficient degree of re-refining was obtained and that although some degree of improvement was observed much better results were almost always obtained when the temperature was increased to a point where incipient azeotropic distillation was noted. Similarly, I have discovered that where very high temperatures were used, that is to say, where a considerable degree of distillation of fatty products was involved. the results of the re-refining process were unsatisfactory, giving a yield which is uneconomicaliy low, and a product which differs substantially from new well-refined oil in chemical characteristics and color. This is shown in the Tables I, II and III by the loss of the oil soluble active substance. The range of operation for satisfactory results embraces approximately 100 F. on either side of the incipient azeotropic distillation point of the hydrocarbons which constitute the major constituent of the compounded oils. For lard cutting oils the range is approximately 200 F. to 400 F.; for sulfur cutting oil, 150 F. to 350 F.; and for sulfur and chlorine cutting oil, 150 F. to 350 F.

Inasmuch as the proportion of oil soluble additive or active agent to the mineral hydrocarbon is usually the most important single property of any compounded oil, the removal or destruction of this additive or agent in a process of re-reflning would very greatly diminish the value of the product. In my process of re-refining utilizing a combined action of distillation and adsorption, under vacuum, I have found that relatively low temperatures are generally suflicient for the removal of contaminating substances such as water, low molecular weight hydrocarbons and decomposition products by distillation and that at these same temperatures, adsorption of the relatively high molecular weight impurities which consist usually of polymerization and resinized products is effected with a high degree of completeness. In the subsequent step of separating or filtering the adsorbent material from the substances being treated all solid particles are removed, including carbonaceous matter and dirt or grit introduced extraneously. If relatively high temperatures are employed. I have found that the proportion of the desired oil soluble additive or active agent maintained is usually greatly diminished. It is not known whether the action is due to increased activity of the adsorbent or to decomposition of the oil soluble agent or to a combination of both of these effects, but the final result is invariably the same. It is, therefore, an important feature oi my invention that I accomplish a high degree of purification of the contaminated compounded oils without injury to any of the constituents or components thereof.

Although I have described my invention with a certain degree of particularity, it is understood that the present disclosure has been made only by way of example and that numerous changes may be resorted to without departing from the spirit and the scope of the invention as hereinafter claimed.

I claim as my invention:

1. The process for removing impurities from a contaminated compounded oil of the class consisting of mineral cutting oils compounded with a lard oil, which process comprises treating the compounded oil without materially affecting the lard oil by mechanically mixing and agitating the contaminated compounded oil and a solid adsorbent material in a sealed container to adsorb the high boiling point impurities, heating the mixture of the compounded oil and the solid adsorbent material in the sealed container under vacuum at a temperature substantially in the range of the incipient azeotropic distillation point of the constituents of the compounded oil being treated to distill off the low boiling point volatile impurities, and separating the adsorbent material with its adsorbed impurities. from the compounded oil being treated to recover the latter.

2. The process for removing impurities from a contaminated compounded oil of the class consisting of mineral oils compounded with an oil soluble sulfur compound, which process comprises treating the compounded oil without materially affecting the oil-soluble sulfur compound by mechanically mixing and agitating the contaminated compounded oil and a solid adsorbent material in a sealed container to adsorb the high boilin point impurities, heating the mixture of the compounded oil and the solid adsorbent material in the sealed container under vacuum at a temperature substantially in the range of the incipient azeotropic distillation point of the constituents of the compounded oil being treated to distill oil! the low boiling point volatile impurities, and separating the adsorbent material with its adsorbed impurities from the compounded oil being treated to recover the latter.

3. The process for removing impurities from a contaminated compounded oil of the class consisting of mineral oils com-pounded with an oilsolubie sulfur' and chlorine compound, which process comprises treating the compounded oil without materially affecting the oil-soluble sulfur and chlorine compound by mechanically mixing and agitating the contaminated compounded oil and a solid adsorbent material in a sealed container to adsorb the high boiling point impurities, heating the mixture of the compounded oil and the solid adsorbent material in the sealed container under vacuum at a temperature substantially in the range of the incipient azeotropic distillation point of the constituents of the compounded oil being treated to distill oil. the low boiling point volatile impurities, and separating the adsorbent material with its adsorbed impurithe mixture oi the compounded oil and the solid adsorbent material in the sealed container under vacuum at a temperature in a range which extends up to substantially 100 F. beyond the incipient azeotropic'distillation point of the constituents of the compounded oil being treated to distill oil the low boiling point volatile impurities, and separating the adsorbent material with its adsorbed impurities from the compounded oil being treated to recover the latter.

5. The process for removing impurities from a contaminated compounded oil of the class conbarometer at sea level and at a temperature in a range which extends up to substantially 400 F. to distill oil the low boiling point volatile im- 1 purities, and separating the adsorbent material sisting of mineral oils compounded with an oilsoluble sulfur compound, which process comprises treating the compounded oil without materiallyaffecting the oil-soluble sulfur compound by mechanically mixing and agitating the contaminated compounded oil and a solid adsorbent material in a sealed container to adsorb the high boiling point impurities, heating the mixture of the compounded oil and the solid adsorbent material in the sealed container under vacuum at a temperature in a range which extends up to substantially 100 F. beyond the incipient azeotropic distillation point of the constituents of the compounded oil being treated to distill oil the low boiling point volatile impurities, and separating the adsorbent material with its adsorbed impurities from the compounded oil being treated to recover the latter.

6. The process for removing impurities from a contaminated compounded oil of the class consisting of mineral oils compounded with an oilsoluble sulfur and chlorine compound, which process comprises treating the compounded oil without materially affecting the oil-soluble sulfur and chlorine compound by mechanically mixing and agitating the contaminated compounded oil and a solid adsorbent material in a sealed container to adsorb the high boiling point impurities, heating the mixture of the compounded oil and the solid adsorbent material in the sealed container under vacuum at a temperature in a range which extends up to substantially 100 F. beyond the incipient azeotropic distillation point of the constituents of the compounded oil being treated to distill off the low boiling point volatile impurities, and separating the adsorbent material with its adsorbed impurities from the compounded oil being treated to recover the latter.

7.- The process for removing impurities from a contaminated compounded oil of the class consisting of mineral cutting oils compounded with a lard oil, which process comprises treating the compounded oil without materially affecting the lard oil by mechanically mixing and agitating the contaminated compounded oil and a solid adsorbent material in a sealed container to adsorb the high boiling point impurities, heating the mixture of the compounded oil' and the solid adsorbent material in the sealed container under vacuum in a range of substantially 28 inches to inches of mercury as referred to a 30 inch with its adsorbed impurities from the compounded oil being treated to recover the latter. v

8. The process for. removing impurities from a contaminated compounded oil of the class con-' sisting of mineral oils compoundedwith an oilsoluble sulfur compound, which process comprises treating-the compounded oil without materially aflecting the oil-soluble sulfur compound by 'mechanically mixing and agitating the contaminated compounded oil and a solid adsorbent ma-- terial in a sealed container to adsorb the high boiling point impurities, heating the mixture of the compounded oil and the solid adsorbent material in the sealed container under vacuum in a range of substantially 28 inches to 30 inches I of mercury as referred to a 30 inch barometer at sea level and at a temperature in a range which extends up to substantially 350 F. to distill oi? the low boiling point volatile impurities, and separating the adsorbent material with its adsorbed impurities from the compounded oil being treated to recover the latter.

9. The process for removing impurities from a contaminated compounded oil of the class consisting of mineral oils compounded with an oilsoluble sulfur and chlorine compound, which process comprises treating the compounded oil without materially aflecting the oil-soluble sulfur and chlorine compound by mechanically mixing and agitating the contaminated compounded oil and a solid adsorbent material in a sealed container to adsorb the high boiling point impurities, heating the mixture of the compounded oil and the solid adsorbent material in the sealed container under vacuum in a range of substantially 28 inches to 30 inches of mercury as referred to a 30 inch barometer at sea level and at a temperature in a range which extends up to substantially 350 F. to distill oil the low boiling point volatile impurities, and separating the adsorbent material with its adsorbed impurities from the compounded oil being treated to recover the latter.

10. The process for removing impurities from a contaminated compounded oil of the class consisting of mineral oils compounded with an oilsoluble additive substance, which process comprises treating the compounded oil without materially affecting any of the constituents thereof by mechanically mixing and agitating the contaminated compounded oil and a solid adsorbent material in a sealed container to adsorb the high boiling point impurities, heating the mixture of the compounded oil and the solid adsorbent material in the sealed container under vacuum at a temperature in'a range which extends up to substantially F. beyond the incipient azeotropic distillation point 01 the constituents of the compounded oil being treated to distill of! the low boiling point volatile impurities, and separating the adsorbent material with its adsorbed impurities from the compounded oil being treated to recover the latter.

11. In a process for removing impurities from a contaminated compounded oil of predominahtly hydro-carbon character and containing minor compounded oil and a solid adsorbent material in a sealed container under'vacuum and subsea contaminated compounded oil the volatile contaminants 11 quently separating with its adsorbed contaminants to recover the compounded oil, the improvement )which consists essentially in subjecting the contaminated compounded oil and the solid adsorbent material toa temperature substantially in the range of the incipient azeotropic distillation point of the constituents of the compounded oil being treated to remove the volatile contaminants by distillation and to adsorb the high boiling point the solid adsorbent before separating the solid adsorbent material with its adsorbed contaminants from the compounded oil to recoverthe latter.

12. In a process for removing impurities from hydro-carbon amounts of an oil-soluble additive compound containing sulfur and chlorine and of contaminatin substances, which comprises mechanically mix-- ing and agitating the contaminated compounded oil 'and a solid ads'orbentmaterial in a sealed container under vacuum and subsequently separating the solid adsorbentmaterial with its adsorbed contaminants to recover improvement which consists essentially in sub- :Iecting the contaminated compounded oil and the solid adsorbent material to a temperature substantially in the range of the incipient azeotropic distillation point of the constituents of the compounded oil being treated to remove the volatile contaminants by distillation and to adsorb the subsequently separating the solid adsorbent material with its adsorbed contaminants to recover the compounded oil, the improvement which consists essentially in subjecting the contaminated compounded oil and the solid adsorbent mate- 'rial to a temperature in a range which extends up to substantially 100 F. beyond the incipient azeotropic distillation. point of the constituents of the compounded oil being treated to remove by distillation and to adsorb the high boiling point impurities by the solid adsorbent before separating the solid adsorbent material-with itsadsorbed contaminants from the compounded oil to recover the latter.

14. In a process for removing'impurities from a contaminated compounded oil of predominantly hydro-carbon character and containing minoramounts of an oil-soluble additive compound containing sulfur and chlorine and of contamiimpurities by 1 character and containing minorthe compounded oil, the

the solid adsorbent materi'al I ll of predominantly azeotropic distillation point 'Of the compounded oil being treated to remove the volatile contaminants by adsorb the high boiling point -so1id adsorbent before separating the solid adnating substances. which-comprises. mechanically mixing and agitating compounded oil and'a solid adsorbent material in -a sealed container under vacuum and subsequently separating the solid adsorbent material with its adsorbed contaminants to recover the compounded oil, the improvement which consists essentlallyiin subjecting the contaminated compounded oil? and the solid adsorbent matein a range which extends 1". beyond'the incipient of the constituents rial to a temperature up to substantially 100 distillation and to impurities by the ,sorbent material with its adsorbed contaminants ess comprises treating out materially affecting from the compounded oil to recover the latter.

15. The process of removing impurities from a contaminated compounded oil of the class consisting of mineral cutting oils compounded with an oil-soluble combination of lard oil and sulfur compounds and chlorine compounds, which procthe compounded oil withthe oil-soluble substances mixing and agitating the contaminated compounded oil with a solid adsorbent material in a sealed container, heating the mixture of the compounded oil and the solid adsorbent material in the sealed container under vacuum at a temperature substantially in the range of the incipient azeotropic distillation point of the constituents of the compounded 011 being treated, whereby the high boiling point impurities are adsorbed by the solid adsorbent material and the low boiling point impurities are distilled on, and thereafter separating the adsorbent material with its adsorbed impurities from the compounded oil being treated to recover the latter.

16. The process of removing impurities from a by mechanically contaminated compounded oil of the class consisting of mineral cutting oils compounded with an oil-soluble combination of lard oil and sulfur compounds'and chlorine compounds, which process comprises treating the compounded oil without materially aflecting the oil-soluble substances by mechanically mixing and agitating the contaminated compounded oil with a solid adsorbent material in a sealedcontainer, heating the mixture of the compounded'oii and the solid adsorbent material in the sealed container under vacuum at a temperature in a range which extends up'to substantially F. beyond the incipient aneotropic distillation point of the constituents of the compounded oil being treated. whereby the high boiling point impurities are adsorbed by the solid adsorbent material and the low boiling point impurities are distilled off, and

.60 thereafter separating the adsorbent material 

